Coal-to-methanol conversion treatment system and coal-to-methanol conversion treatment simulation method

Abstract

The invention discloses a coal-to-methanol conversion treatment system and a coal-to-methanol conversion treatment simulation method. The coal-to-methanol conversion treatment system comprises a gas separator, a conversion furnace, a first water separation device, a stripping tower and a second water separation device. Water gas of a gasification section enters a gas separator, and a gas phase discharged from a gas outlet of the gas separator is divided into a first gas phase and a second gas phase through a flow divider; the inlet of the conversion furnace is connected with the flow divider so that the first gas phase flows into the conversion furnace; the first water separation device is used for performing multi-stage separation on the mixed gas; steam entering the stripping tower from the steam inlet is in contact with condensate entering the stripping tower from the first water separation device; and the second water separation device is connected with the gas outlet of the stripping tower to separate the vent gas and the wastewater. Water gas can be effectively treated, so that the energy consumption of the system is reduced, the water-saving and environment-friendly effects are achieved, and the purposes of improving quality and efficiency can be achieved.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of chemical industry, and particularly relates to a coal-to-methanol shift processing system and a coal-to-methanol shift processing simulation method. BACKGROUND

[0002] The molar ratio of hydrogen to carbon monoxide in the crude coal gas obtained by coal gasification is between 0.2 and 3.0. Since the methanol synthesis process has strict requirements on the molar ratio of hydrogen to carbon monoxide in the raw gas, the synthesis gas obtained by coal gasification needs to be subjected to a steam shift unit to convert part of the carbon monoxide into hydrogen by using steam so as to adjust the composition ratio of the synthesis gas to a suitable value.

[0003] Under the background of energy saving and emission reduction, starting from the production process, process system simulation is carried out to optimize the operation parameters and process, and based on this, energy saving, consumption reduction, emission reduction and environmental protection are guided, which is of great significance for enterprise quality improvement and efficiency increase, water saving and environmental protection. SUMMARY

[0004] The present application aims to at least partially solve one of the technical problems in the related art.

[0005] To this end, the embodiments of the present application propose a coal-to-methanol shift processing system with low energy consumption, good water saving and environmental protection effects.

[0006] The embodiments of the present application propose a coal-to-methanol shift processing simulation method.

[0007] The coal-to-methanol shift processing system of the embodiments of the present application comprises:

[0008] A coal gas separator, a shunt is connected to the gas outlet of the coal gas separator, the water gas of the gasification section enters the coal gas separator, and the gas phase discharged from the gas outlet of the coal gas separator is divided into a first gas phase and a second gas phase by the shunt;

[0009] A shift furnace, the inlet of the shift furnace is connected to the shunt so that the first gas phase flows into the shift furnace, and a preheater is arranged between the inlet of the shift furnace and the shunt to heat the first gas phase flowing into the shift furnace;

[0010] A first water separation device, the first water separation device is connected to the shunt and the shift furnace, so that the mixed gas after the mixing of the second gas phase and the gas stream discharged from the shift furnace flows into the first water separation device, and the first water separation device is used to perform multi-stage separation on the mixed gas to obtain shift gas and condensate;

[0011] a stripping tower, an inlet of the stripping tower being connected with the first water separation device so that at least part of the condensed liquid discharged by the first water separation device flows into the stripping tower, the stripping tower having a steam inlet, steam entering the stripping tower from the steam inlet being in contact with the condensed liquid entering the stripping tower from the first water separation device to recover combustible gas dissolved in the condensed liquid, condensed liquid discharged from a liquid outlet of the stripping tower flowing back to the gasification section;

[0012] a second water separation device, an air outlet of the second water separation device being connected with an air outlet of the stripping tower to separate out vent air and waste water.

[0013] The coal-to-methanol shift processing system can effectively process water gas, thereby reducing energy consumption of the system, achieving water-saving and environmental protection effects, and achieving the purpose of quality improvement and efficiency increase.

[0014] In some embodiments, a first mixer is further included, the first mixer being connected with the flow divider and an outlet of the shift converter, a cold side flow channel of the preheater being connected between the flow divider and an inlet of the shift converter, and a hot side flow channel of the preheater being connected between the shift converter and the first mixer.

[0015] In some embodiments, a first waste heat boiler is arranged between an outlet of the shift converter and the first mixer, and a second waste heat boiler is arranged between an outlet of the first mixer and the first water separation device.

[0016] In some embodiments, the first water separation device comprises:

[0017] a first water separator, an inlet of the first water separator being connected with the flow divider and the shift converter;

[0018] a second water separator, an inlet of the second water separator being connected with an air outlet of the first water separator, and liquid discharged from a liquid outlet of the first water separator and a liquid outlet of the second water separator flowing back to the gasification section;

[0019] a third water separator, an inlet of the third water separator being connected with an air outlet of the second water separator;

[0020] a fourth water separator, an inlet of the fourth water separator being connected with an air outlet of the third water separator, and a liquid outlet of the third water separator and a liquid outlet of the fourth water separator being connected with an inlet of the stripping tower.

[0021] In some embodiments, a third waste heat boiler is arranged between the gas outlet of the first water separator and the inlet of the second water separator, a desalted water heater is arranged between the gas outlet of the second water separator and the inlet of the third water separator, and a shift gas cooler is arranged between the gas outlet of the third water separator and the inlet of the fourth water separator.

[0022] The liquid outlet of the first water separator and the liquid outlet of the second water separator are connected with a second mixer, and the outlet of the second mixer is connected with a first pump.

[0023] In some embodiments, a third mixer and a condensate heater are arranged between the liquid outlet of the third water separator and the liquid outlet of the fourth water separator, and the condensate heater is connected with the stripping column so that the condensate discharged from the third mixer flows into the stripping column after being heated.

[0024] In some embodiments, the cold side flow channel of the condensate heater is connected between the third mixer and the stripping column, the hot side flow channel of the condensate heater is connected to the liquid outlet of the stripping column, so that the liquid flowing out of the liquid outlet of the stripping column heats the condensate flowing from the third mixer to the stripping column, and the liquid outlet of the stripping column is connected with a second pump.

[0025] In some embodiments, the second water separation device comprises a fifth water separator, the inlet of the fifth water separator is connected with the gas outlet of the stripping column, and a water cooler is arranged between the inlet of the fifth water separator and the gas outlet of the stripping column.

[0026] In some embodiments, the steam inlet comprises a first steam inlet and a second steam inlet, the first steam inlet is used to deliver low-pressure steam from a pipe network into the stripping column, and the second steam inlet is used to deliver high-pressure flash steam from a gasification section into the stripping column, and the steam delivered into the stripping column flows in a reverse direction with the condensate.

[0027] The coal-to-methanol shift processing simulation method of the embodiments of the present application is used to optimize the coal-to-methanol shift processing system as described in any one of the above embodiments, and the coal-to-methanol shift processing simulation method comprises:

[0028] Based on the coal-to-methanol shift processing system, a mathematical model is constructed by using Aspen Plus software;

[0029] Given the running information, the mathematical model is run, and a simulation result report is obtained;

[0030] The actual running condition is compared with the simulation result report, and the last step is repeated to obtain the final running information of the mathematical model;

[0031] adjust at least part of operation parameters of the mathematical model to obtain a target result report;

[0032] determine whether the target result operation meets the requirement;

[0033] if yes, adjust actual operation condition parameters of the coal-to-methanol shift processing system based on the target result report.

[0034] In some embodiments, the step of constructing the mathematical model utilizes Aspen Plus software, including:

[0035] based on the material components of water gas, when the temperature is less than or equal to 100 degrees Celsius, the gas-liquid separation device in the mathematical model adopts electrolyte property method ELECNRTL, the liquid phase activity coefficient calculation method is Electrolyte NRTL, and the gas phase fugacity coefficient calculation method is Redlich-Kwong, when the temperature is less than or equal to 100 degrees Celsius, the gas-liquid separation device in the mathematical model adopts electrolyte property method RK-SOAVE;

[0036] based on the physical properties and process requirements of each device in the coal-to-methanol shift processing system, select the corresponding unit operation module in the Aspen Plus software;

[0037] based on the characteristics of heat flow, material flow and power flow in the coal-to-methanol shift processing system, select the corresponding thermodynamic model and property database in the Aspen Plus software.

[0038] In some embodiments, in the final operation information, the unit operation module adopted by the coal water separator, the first water separator, the second water separator, the third water separator, the fourth water separator and the fifth water separator in the coal-to-methanol shift processing system is Flash2, the unit operation module adopted by the shift furnace in the coal-to-methanol shift processing system is RSoic, the unit operation module adopted by the stripping tower in the coal-to-methanol shift processing system is Flash2, the unit operation module adopted by the first mixer, the second mixer and the third mixer in the coal-to-methanol shift processing system is Mixer, and the unit operation module adopted by the first pump and the second pump in the coal-to-methanol shift processing system is Pump;

[0039] In the mathematical model built by the Aspen Plus software, the operating pressure of the coal water separator is 6.34 MPa, the operating temperature is 243 degrees Celsius, the operating pressure of the first water separator is 6.06 MPa, the operating temperature is 216.5 degrees Celsius, the operating pressure of the second water separator is 6.02 MPa, the operating temperature is 190 degrees Celsius, the operating pressure of the third water separator is 5.97 MPa, the operating temperature is 106 degrees Celsius, the operating pressure of the fourth water separator is 5.91 MPa, the operating temperature is 40 degrees Celsius, the operating pressure of the fifth water separator is 0.41 MPa, and the operating temperature is 45 degrees Celsius;

[0040] The operating pressure of the reformer is 6.14 MPa, and the operating temperature is 441 degrees Celsius; the operating pressure of the stripping tower is 0.49 MPa, and the operating temperature is 147 degrees Celsius;

[0041] The outlet pressure of the first mixer is 6.11 MPa, the outlet pressure of the second mixer is 6.02 MPa, the outlet pressure of the third mixer is 0.53 MPa, the outlet pressure of the first pump is 7.2 MPa, and the outlet pressure of the second pump is 1.6 MPa.

[0042] In some embodiments, the first waste heat boiler, the second waste heat boiler, the third waste heat boiler, the desalted water heater, the shift gas cooler, and the water cooler in the coal-to-methanol shift processing system all adopt a Heater unit operation module, a first heat exchange operation module is arranged between the splitter and the inlet of the reformer, a second heat exchange operation module is arranged between the outlet of the reformer and the first mixer, the first heat exchange operation module and the second heat exchange operation module are connected to constitute a preheater in the coal-to-methanol distillation system, a third heat exchange operation module is arranged between the third mixer and the inlet of the stripping tower, a fourth heat exchange operation module is connected to the outlet of the stripping tower, the third heat exchange operation module and the fourth heat exchange operation module are connected to constitute a condensate heater in the coal-to-methanol distillation system, and the first heat exchange operation module, the second heat exchange operation module, the third heat exchange operation module, and the fourth heat exchange operation module all adopt a Heater;

[0043] In the mathematical model built by the Aspen Plus software, the operating pressure of the first waste heat boiler is 6.11 MPa, the operating temperature is 240 degrees Celsius, the operating pressure of the second waste heat boiler is 6.07 MPa, the operating temperature is 216.5 degrees Celsius, the operating pressure of the third waste heat boiler is 6.03 MPa, the operating temperature is 190 degrees Celsius, the operating pressure of the desalted water heater is 5.98 MPa, the operating temperature is 106 degrees Celsius, the operating pressure of the shift gas cooler is 5.92 MPa, the operating temperature is 40 degrees Celsius, the operating pressure of the water cooler is 0.42 MPa, the operating temperature is 45 degrees Celsius, the operating pressure of the first heat exchange operation module is 6.22 MPa, the operating temperature is 250 degrees Celsius, the operating pressure of the second heat exchange operation module is 6.13 MPa, the operating pressure of the third heat exchange operation module is 0.53 MPa, and the operating pressure of the fourth heat exchange operation module is 0.48 MPa, the operating temperature is 95 degrees Celsius. BRIEF DESCRIPTION OF DRAWINGS

[0044] Figure 1 Fig. 1 is a schematic diagram of a coal-to-methanol shift processing system according to an embodiment of the present application.

[0045] Figure 2 Fig. 2 is a flow chart of a coal-to-methanol shift processing simulation method according to an embodiment of the present application.

[0046] REFERENCE NUMERALS:

[0047] 11, coal gas separator; 12, flow divider;

[0048] 21, shift furnace;

[0049] 31, first water separator; 32, second water separator; 33, third water separator; 34, fourth water separator;

[0050] 41, stripping column;

[0051] 51, fifth water separator;

[0052] 61, first mixer; 62, first waste heat boiler; 63, second waste heat boiler; 64, third waste heat boiler; 65, second mixer; 66, third mixer; 67, condensate heater; 671, third heat exchange operation module; 672, fourth heat exchange operation module; 68, water cooler; 69, desalted water heater; 70, shift gas cooler;

[0053] 71, first pump; 72, second pump;

[0054] 8, preheater; 81, first heat exchange operation module; 82, second heat exchange operation module. DETAILED DESCRIPTION

[0055] Embodiments of the present application are described in detail below with reference to the attached drawing figures, wherein like reference numerals refer to like elements throughout. The embodiments described below are illustrative examples of how the present application can be put into practice. They should not be considered in any way to restrict the present application, the scope of which should be determined by reference to the appended claims.

[0056] Referring to Figure 1 The coal-to-methanol shift processing system of the embodiments of the present application comprises a coal gas separator 11, a shift furnace 21, a first water separation device, a stripping column 41 and a second water separation device.

[0057] The coal gas separator 11 is connected with a flow divider 12, and the water gas from the gasification section enters the coal gas separator 11, and the gas phase discharged from the outlet of the coal gas separator 11 is divided into a first gas phase and a second gas phase by the flow divider 12. The first gas phase and the second gas phase can be divided into two gas streams in a preset ratio.

[0058] The inlet of the shift furnace 21 is connected with the flow divider 12 to make the first gas phase flow into the shift furnace 21, and a preheater 8 is arranged between the inlet of the shift furnace 21 and the flow divider 12 to heat the first gas phase flowing into the shift furnace 21. The preheater 8 is used to heat the first gas phase and deliver the heated first gas phase into the shift furnace 21. For example, the preheater 8 can heat the gas stream of the first gas phase to 315 degrees Celsius and then deliver it into the shift furnace 21, and the temperature in the shift furnace 21 is set to 441 degrees Celsius and the pressure is 6.04 MPa.

[0059] The first water separation device is connected with the flow divider 12 and the shift furnace 21 to make the mixed gas after the second gas phase and the gas stream discharged from the shift furnace 21 are mixed flow into the first water separation device, and the first water separation device is used to carry out multi-stage separation on the mixed gas to obtain shift gas and condensate. That is to say, the outlet gas stream of the shift furnace 21 is mixed with the unshifted second gas phase and then delivered into the first water separation device.

[0060] In the multi-stage separation process, part of the condensate produced can be delivered into the stripping column 41, and the other part of the condensate separated out without value can be delivered to sewage treatment.

[0061] The inlet of the stripping column 41 is connected with the first water separation device to make at least part of the condensate discharged from the first water separation device flow into the stripping column 41, and the stripping column 41 has a steam inlet, the steam entering the stripping column 41 from the steam inlet contacts the condensate entering the stripping column 41 from the first water separation device to recover the combustible gas dissolved in the condensate, and the condensate discharged from the liquid outlet of the stripping column 41 flows back to the gasification section.

[0062] The second water separation device is connected with the gas outlet of the stripping column 41 to separate out vent gas and waste water.

[0063] The coal-to-methanol shift processing system can effectively process water gas, thereby reducing energy consumption of the system, realizing water saving and environmental protection effect, and achieving the purpose of quality improvement and efficiency increase.

[0064] In some embodiments, the coal-to-methanol shift processing system further comprises a first mixer 61 connected with the shunt 12 and the outlet of the shift converter 21, the cold side flow channel of the preheater 8 is connected between the inlet of the shunt 12 and the shift converter 21, and the hot side flow channel of the preheater 8 is connected between the shift converter 21 and the first mixer 61. The preheater 8 can use the waste heat of the fluid discharged from the shift converter 21 to heat the first gas phase entering the shift converter 21, thereby realizing heat recycling.

[0065] The outlet of the shift converter 21 is connected with a first waste heat boiler 62, and the outlet of the first mixer 61 is connected with a second waste heat boiler 63. The first waste heat boiler 62 can further recycle the heat in the fluid discharged from the shift converter 21. When the second gas phase is mixed with the gas stream discharged from the shift converter 21 by the first mixer 61, the heat of the gas stream is recycled by the second waste heat boiler 63, thereby further cooling the fluid.

[0066] For example, the fluid discharged from the shift converter 21 can be cooled to 240 degrees Celsius after passing through the preheater 8 and the first waste heat boiler 62 of 2.5 MPa, then mixed with the second gas phase, cooled to 216.5 degrees Celsius by the second waste heat boiler 63 of 1.0 MPa, and finally enters the first water separation device. Thus, not only the heat is recycled, but also the shift processing of the water gas is realized.

[0067] In some embodiments, the first water separation device comprises a first water separator 31, a second water separator 32, a third water separator 33, and a fourth water separator 34.

[0068] The inlet of the first water separator 31 is connected with the shunt 12 and the shift converter 21; specifically, the inlet of the first water separator 31 is connected with the second waste heat boiler 63, and the mixed fluid cooled by the second waste heat boiler 63 flows into the first water separator 31. The first water separator 31 performs primary separation on the mixed fluid.

[0069] The inlet of the second water separator 32 is connected with the gas outlet of the first water separator 31 to perform secondary separation. In this embodiment, the third waste heat boiler 64 is arranged between the gas outlet of the first water separator 31 and the inlet of the second water separator 32. The third waste heat boiler 64 with a pressure of 0.5 MPa can cool the fluid at the gas outlet of the first water separator 31 to 190 degrees Celsius. The liquid discharged from the liquid outlet of the first water separator 31 and the liquid outlet of the second water separator 32 is returned to the gasification section to recover the condensate of the first water separator 31 and the second water separator 32. The second mixer 65 is connected with the liquid outlet of the first water separator 31 and the liquid outlet of the second water separator 32. The outlet of the second mixer 65 is connected with the first pump 71.

[0070] The inlet of the third water separator 33 is connected with the gas outlet of the second water separator 32 to perform tertiary separation. The inlet of the fourth water separator 34 is connected with the gas outlet of the third water separator 33 to perform quaternary separation. The desalted water heater 69 is arranged between the gas outlet of the second water separator 32 and the inlet of the third water separator 33. The desalted water heater 69 can cool the gas stream at the gas outlet of the second water separator 32 to 106 degrees Celsius. The shift gas cooler 70 is arranged between the gas outlet of the third water separator 33 and the inlet of the fourth water separator 34. The shift gas cooler 70 can cool the gas stream separated by the third water separator 33 to about 40 degrees Celsius.

[0071] The fluid entering the fourth water separator 34 is mixed with a certain flow of feed water from the high-pressure boiler. The temperature of the feed water is about 133.5 degrees Celsius, and the feed water is cooled to about 40 degrees Celsius before entering the fourth water separator 34. In the fourth water separator 34, shift gas can be separated, with a temperature of about 40 degrees Celsius and a pressure of 5.81 MPa.

[0072] The liquid outlet of the third water separator 33 and the liquid outlet of the fourth water separator 34 are connected with the inlet of the stripping column 41 to further process the condensate of the third water separator 33 and the fourth water separator 34 through the stripping column 41. The third mixer 66 and the condensate heater 67 are connected with the liquid outlet of the third water separator 33 and the liquid outlet of the fourth water separator 34. The condensate heater 67 is connected with the stripping column 41 to make the condensate discharged from the third mixer 66 flow into the stripping column 41 after being heated. The condensate heater 67 can heat the liquid to about 128 degrees Celsius, and then the liquid enters the stripping column 41.

[0073] In this embodiment, multi-stage separation is realized through different temperature control and the cooperation of multiple water separators, high-quality shift gas and condensate are obtained, and thus the treatment effect is improved.

[0074] In some embodiments, the cold side flow channel of the condensate heater 67 is connected between the third mixer 66 and the stripping tower 41, and the hot side flow channel of the condensate heater 67 is connected to the liquid outlet of the stripping tower 41, so that the liquid flowing out of the liquid outlet of the stripping tower 41 can heat the condensate flowing from the third mixer 66 to the stripping tower 41, and the liquid outlet of the stripping tower 41 is connected with the second pump 72, so that the heat can be recycled and the energy consumption can be reduced. The condensate discharged from the stripping tower 41 can heat the condensate entering the stripping tower 41 to about 95 degrees Celsius, and the condensate discharged from the stripping tower 41 is also delivered to the gasification section as process condensate.

[0075] The steam inlet of the stripping tower 41 includes a first steam inlet and a second steam inlet, the first steam inlet is used to deliver the low-pressure steam of the pipe network into the stripping tower 41, and the second steam inlet is used to deliver the high-pressure flash steam of the gasification section into the stripping tower 41, and the steam delivered into the stripping tower 41 flows in the opposite direction of the condensate. Thus, the combustible gas dissolved in the condensate can be recycled, the utilization rate of heat can be improved, the energy consumption can be reduced, and the recycling rate of the combustible gas can be improved.

[0076] Further, the second water separation device includes a fifth water separator 51, the inlet of the fifth water separator 51 is connected with the gas outlet of the stripping tower 41, and a water cooler 68 is arranged between the inlet of the fifth water separator 51 and the gas outlet of the stripping tower 41. The vent gas at the top of the stripping tower 41 is cooled to about 45 degrees Celsius by the water cooler 68 and then separated into steam and water by the fifth water separator 51, the separated gas is sent to a flare for combustion, and the condensate is delivered to a sewage treatment.

[0077] Referring to Figure 1 and Figure 2 , the coal-to-methanol shift processing simulation method of the embodiment of the present application is used for optimizing the coal-to-methanol shift processing system as in any one of the above, and the coal-to-methanol shift processing simulation method comprises:

[0078] S101, based on the coal-to-methanol shift processing system, a mathematical model is constructed by using Aspen Plus software.

[0079] According to the design process flow diagram, the unit operation module is selected to represent the equipment or device in the actual plant, the selected operation module is connected by heat flow, material flow and work flow, and finally the completeness of the flow is determined and checked.

[0080] In Aspen Plus, the crude methanol distillation unit typically involves the following main equipment or devices: Heater: used to heat the feed or intermediate streams. Mixer: used to mix different streams. RadFrac: used to separate methanol and other components. Heater: requires setting parameters such as heating temperature, pressure, heat duty, etc. Mixer: requires setting parameters such as mixing ratio, temperature and pressure after mixing, etc. RadFrac: requires setting parameters such as number of stages, feed location, reflux ratio, specifications of overhead and bottom products, etc.

[0081] When selecting models and setting parameters, reference is usually made to actual process flows, experimental data and literature to improve separation efficiency and reduce energy consumption. How to accurately predict tray efficiency, how to handle non-ideal mixture phase equilibrium, how to optimize heat integration to reduce energy consumption, etc. can be overcome through iterative simulation and experimental verification.

[0082] In Aspen Plus, the conversion unit model of the coal-to-methanol process involves multiple equipment or devices such as "Heater", "Mixer", "Flash2", etc. Although these devices may use the same model in Aspen Plus (such as "Heater" for heaters, heat exchangers, etc.), their parameter settings will vary depending on the function and operating conditions of the specific equipment. Heater: used to simulate heating or cooling processes, usually used to preheat reactants or cool products. The selection is based on the heat duty and temperature range of the equipment. Mixer: used to simulate mixing processes, usually used to mix different streams. The selection is based on the uniformity of mixing and the properties of the mixed stream. Flash2: used to simulate flash processes, usually used to separate gas-liquid two-phase. The selection is based on separation efficiency and phase equilibrium conditions.

[0083] The operating conditions of different equipment (such as temperature, pressure, flow rate, etc.) vary greatly and need to be accurately set according to the actual process conditions. For example, the heat duty and temperature range of the heater need to be optimized according to the reaction conditions.

[0084] Some equipment may require more complex models to accurately simulate their behavior. For example, a reactor may need to use the "REAC" module instead of a simple "Heater" or "Mixer".

[0085] When selecting unit operation modules for heat flow, material flow and power flow, in the coal-to-methanol process, the main heat flow, material flow and power flow include:

[0086] Heat flow: reaction heat, heat duty of heat exchanger, heat duty of cooler, etc.

[0087] Material flow: raw coal, steam, synthesis gas, methanol, etc.

[0088] Work streams: Power consumption of equipment such as compressors, pumps, etc.

[0089] In the corresponding unit operation modules in Aspen Plus, heat streams: Heater is used to simulate heating or cooling processes, such as preheaters, coolers, etc. HeatX is used to simulate heat exchangers, such as reactor feed preheaters, product coolers, etc.

[0090] Material streams: Mixer is used to simulate mixing processes, such as the mixing of raw coal and steam. Flash2 is used to simulate flash processes, such as the separation of synthesis gas and methanol.

[0091] Work streams: Compr is used to simulate compressors, such as synthesis gas compressors. Pump is used to simulate pumps, such as methanol delivery pumps.

[0092] Select appropriate modules according to process requirements to ensure the accuracy of the simulation. For example, use the "HeatX" module instead of "Heater" to simulate complex heat exchange processes. Optimize module parameters (such as heat transfer coefficients of heat exchangers, efficiencies of compressors, etc.) to improve the accuracy of the simulation.

[0093] The coal-to-methanol process involves multiple reactions and separation processes, requiring the use of multiple modules to ensure the matching of material and heat streams between modules. Some parameters (such as reaction rates, heat transfer coefficients, etc.) may have uncertainties and need to be calibrated through experimental data or literature data.

[0094] Select appropriate calculation formulas according to specific process conditions to ensure the accuracy of the calculation. For example, use the reaction heat formula to calculate the heat load of the reactor. Calibrate parameters (such as heat capacity, reaction heat, etc.) in the formula through experimental data or literature data to improve the accuracy of the calculation. The coal-to-methanol process involves multiple reactions and separation processes, requiring the use of multiple formulas to ensure matching between formulas. Some parameters (such as reaction heat, heat transfer coefficient, etc.) may have uncertainties and need to be calibrated through experimental data or literature data.

[0095] When simulating the variable unit model of the coal-to-methanol process in Aspen Plus, the selection and parameter setting of the equipment model are key. By accurately selecting modules and optimizing parameters, the difficulties of process complexity and parameter uncertainty can be overcome. At the same time, the calculation formulas of material streams, work streams, and heat streams provide a theoretical basis for simulation, ensuring the accuracy and reliability of the simulation.

[0096] S102, given the running information, run the mathematical model, and obtain the simulation result report.

[0097] The specified components, the given each stream and the parameter components of the established unit module are generally divided into: conventional inert solids, conventional components and unconventional solids.

[0098] The step of constructing a mathematical model by using the Aspen Plus software includes:

[0099] Based on the material components of the water-gas, when the temperature is less than or equal to 100 degrees Celsius, the electrolyte property method ELECNRTL is used in the mathematical model of the gas-liquid separation device, the liquid phase activity coefficient calculation method is Electrolyte NRTL, and the gas phase fugacity coefficient calculation method is Redlich-Kwong.

[0100] The substances involved in the embodiment of the present application are CO2, H2, CO, H2O, CH3OH, CH4, N2 and Ar, CO2 and NH3 contained in the coal gas are partially dissolved in the liquid with water as the main component, the dissolved CO2 and NH3 will chemically react under the action of water molecules, since the concentration of CO2 is much higher than that of NH3, ammonium bicarbonate will be mainly produced in the water solution, since the ammonium bicarbonate ionizes in the water solution, therefore, the electrolyte property method ELECNRTL should be used in each gas-liquid separator, the liquid phase activity coefficient calculation method is Electrolyte NRTL, and the gas phase fugacity coefficient calculation method is Redlich-Kwong.

[0101] Based on the physical properties and process requirements of each device in the coal-to-methanol shift processing system, corresponding unit operation modules are selected in the Aspen Plus software.

[0102] Based on the characteristics of heat flow, material flow and power flow in the coal-to-methanol shift processing system, corresponding thermodynamic models and property databases are selected in the Aspen Plus software.

[0103] S103, the actual operation condition and the simulation result report are compared, and the previous step is repeated to obtain the final operation information of the mathematical model.

[0104] In the final operation information, the unit operation module adopted by the coal water separator, the first water separator 31, the second water separator 32, the third water separator 33, the fourth water separator 34, and the fifth water separator 51 in the coal-to-methanol conversion processing system is Flash2, the unit operation module adopted by the conversion furnace 21 in the coal-to-methanol conversion processing system is RSoic, the unit operation module adopted by the stripping column 41 in the coal-to-methanol conversion processing system is Flash2, the unit operation module adopted by the first mixer 61, the second mixer 65, and the third mixer 66 in the coal-to-methanol conversion processing system is Mixer, and the unit operation module adopted by the first pump 71 and the second pump 72 in the coal-to-methanol conversion processing system is Pump.

[0105] In the mathematical model built by the AspenPlus software, the operating pressure of the coal water separator is 6.34 MPa, and the operating temperature is 243 degrees Celsius; the operating pressure of the first water separator 31 is 6.06 MPa, and the operating temperature is 216.5 degrees Celsius; the operating pressure of the second water separator 32 is 6.02 MPa, and the operating temperature is 190 degrees Celsius; the operating pressure of the third water separator 33 is 5.97 MPa, and the operating temperature is 106 degrees Celsius; the operating pressure of the fourth water separator 34 is 5.91 MPa, and the operating temperature is 40 degrees Celsius; the operating pressure of the fifth water separator 51 is 0.41 MPa, and the operating temperature is 45 degrees Celsius; the operating pressure of the conversion furnace 21 is 6.14 MPa, and the operating temperature is 441 degrees Celsius; the operating pressure of the stripping column 41 is 0.49 MPa, and the operating temperature is 147 degrees Celsius; the outlet pressure of the first mixer 61 is 6.11 MPa, the outlet pressure of the second mixer 65 is 6.02 MPa, the outlet pressure of the third mixer 66 is 0.53 MPa, the outlet pressure of the first pump 71 is 7.2 MPa, and the outlet pressure of the second pump 72 is 1.6 MPa.

[0106] The unit operation modules used in the first waste heat boiler 62, the second waste heat boiler 63, the third waste heat boiler 64, the desalted water heater 69, the shift gas cooler 70, and the water cooler 68 in the shift conversion system of the coal-to-methanol system are all Heaters. A first heat exchange operation module 81 is arranged between the splitter 12 and the inlet of the shift converter 21, a second heat exchange operation module 82 is arranged between the outlet of the shift converter 21 and the first mixer 61, the first heat exchange operation module 81 and the second heat exchange operation module 82 are connected to form a preheater 8 in the coal-to-methanol distillation system, a third heat exchange operation module 671 is arranged between the third mixer 66 and the inlet of the stripping column 41, and a fourth heat exchange operation module 672 is connected to the liquid outlet of the stripping column 41, the third heat exchange operation module 671 and the fourth heat exchange operation module 672 are connected to form a condensate heater 67 in the coal-to-methanol distillation system, and the first heat exchange operation module 81, the second heat exchange operation module 82, the third heat exchange operation module 671, and the fourth heat exchange operation module 672 are all Heaters.

[0107] In the mathematical model built by the AspenPlus software, the operating pressure of the first waste heat boiler 62 is 6.11 MPa, and the operating temperature is 240 degrees Celsius, the operating pressure of the second waste heat boiler 63 is 6.07 MPa, and the operating temperature is 216.5 degrees Celsius, the operating pressure of the third waste heat boiler 64 is 6.03 MPa, and the operating temperature is 190 degrees Celsius, the operating pressure of the desalted water heater 69 is 5.98 MPa, and the operating temperature is 106 degrees Celsius, the operating pressure of the shift gas cooler is 5.92 MPa, and the operating temperature is 40 degrees Celsius, the operating pressure of the water cooler 68 is 0.42 MPa, and the operating temperature is 45 degrees Celsius, the operating pressure of the first heat exchange operation module 81 is 6.22 MPa, and the operating temperature is 250 degrees Celsius, the operating pressure of the second heat exchange operation module 82 is 6.13 MPa, the operating pressure of the third heat exchange operation module 671 is 0.53 MPa, the operating pressure of the fourth heat exchange operation module 672 is 0.48 MPa, and the operating temperature is 95 degrees Celsius.

[0108] S104, adjusting at least part of the running parameters of the mathematical model to obtain a target result report.

[0109] S105, judging whether the target result running meets the requirements.

[0110] S106, if yes, adjusting the actual running condition parameters of the shift conversion system of the coal-to-methanol system based on the target result report.

[0111] Example 1: Adjusting reactor operating conditions, the adjustment parameters include reaction temperature (Temperature), reaction pressure (Pressure), feed gas composition (such as the ratio of CO, H2, CO2), etc. By adjusting the reaction temperature, the conversion rate and selectivity of methanol synthesis reaction can be optimized. For example, increasing the temperature may accelerate the reaction rate, but too high temperature may lead to an increase in side reactions. Adjusting the pressure can affect the reaction equilibrium, higher pressure is generally beneficial to the progress of methanol synthesis reaction. Adjusting the feed gas composition (such as H2 / CO ratio) can optimize the utilization of reactants and reduce the amount of unreacted gas circulation.

[0112] The effect achieved is: optimizing the operating conditions of the reactor, improving the methanol production and reaction efficiency. In actual modification, the heating / cooling system or gas compression system of the reactor may need to be adjusted to adapt to the new operating conditions.

[0113] Example 2: Adjusting the design parameters of the heat exchanger, the adjustment parameters include: heat transfer area of the heat exchanger (Heat Transfer Area), overall heat transfer coefficient of the heat exchanger (Overall Heat Transfer Coefficient, U), flow rate and temperature of cold and hot fluids, etc. By increasing the heat transfer area or improving the heat transfer coefficient, the heat transfer effect can be enhanced and the energy consumption can be reduced. Adjusting the flow rate and temperature of cold and hot fluids can optimize the heat recovery efficiency and reduce the need for external heating or cooling.

[0114] The effect achieved is: according to the simulation results, optimizing the design of the heat exchanger, such as increasing the heat transfer area or improving the structure of the heat exchanger. In actual modification, the existing heat exchanger may need to be replaced or upgraded to improve energy utilization efficiency.

[0115] Example 3: Adjusting the operating conditions of the separation unit, the adjustment parameters include: flash tank operating pressure (Flash Pressure), separation temperature (Flash Temperature), feed composition (Feed Composition). By adjusting the pressure and temperature of the flash tank, the gas-liquid separation effect can be optimized and the recovery rate of methanol can be improved. By changing the feed composition, the influence on the separation efficiency can be analyzed, for example, high CO2 content may lead to increased difficulty in separation.

[0116] The effect achieved is: according to the simulation results, optimizing the operating conditions of the flash tank, improving the purity and recovery rate of methanol. In actual modification, the pressure control system of the flash tank may need to be adjusted or a pretreatment step (such as CO2 removal) may need to be added.

[0117] Example 4: Adjusting recycle stream parameters, including: recycle ratio, recycle composition, etc. Increasing the recycle ratio can improve raw material utilization, but may lead to increased equipment load. Adjusting the composition of the recycle stream (e.g., H2 / CO ratio) can optimize the feed conditions for the reactor, improving reaction efficiency.

[0118] The achieved effect is: According to the simulation results, optimize the management of the recycle stream, balance the raw material utilization and equipment load. In actual modification, it may be necessary to upgrade the recycle compressor or adjust the gas purification system.

[0119] Example 5: Adjusting energy integration schemes, including: temperature intervals of heat integration networks, heat and cold stream matching, etc. By optimizing the heat integration network, the demand for external heating and cooling can be reduced, and energy consumption can be reduced. Adjusting the matching of hot and cold streams can improve heat recovery efficiency.

[0120] The achieved effect is: According to the simulation results, design a more efficient heat integration scheme, such as adding heat exchangers or optimizing the heat recovery network. In actual modification, it may be necessary to redesign the heat exchange network of the plant or upgrade existing equipment.

[0121] Example 6: Adjusting catalyst performance parameters, including: catalyst activity, catalyst selectivity, etc. Increasing catalyst activity can speed up the reaction rate, but may lead to an increase in side reactions. Optimizing catalyst selectivity can improve the yield of methanol and reduce the generation of by-products.

[0122] The achieved effect is: According to the simulation results, select the appropriate catalyst or optimize the use conditions of the catalyst. In actual modification, it may be necessary to replace the catalyst or adjust the operating conditions of the reactor.

[0123] Example 7: Adjusting the operating parameters of compressors and pumps, including: compression ratio of compressors, pump head and flow rate, etc. Adjusting the compression ratio can optimize the energy consumption of gas compression, but too high compression ratio may lead to increased equipment load. Adjusting the pump head and flow rate can optimize the efficiency of liquid delivery.

[0124] The effect achieved is: according to the simulation results, the operating conditions of the compressor and the pump are optimized, and the energy consumption is reduced. In actual modification, the compressor and the pump may need to be upgraded, or their operating parameters may need to be adjusted.

[0125] The modification cases in practical application are:

[0126] 1. Reactor optimization:

[0127] Through simulation, it is found that increasing the reaction temperature from 240 DEG C to 260 DEG C can increase the methanol yield, but the side reaction increases. Therefore, in actual modification, a segmented temperature control strategy is adopted, which not only increases the yield, but also controls the side reaction.

[0128] 2. Heat integration modification:

[0129] The simulation results show that by optimizing the heat integration network, the external heating demand can be reduced by about 15%. In actual modification, new heat exchangers are added and the heat recovery network is optimized, which significantly reduces the energy consumption.

[0130] 3. Separation unit upgrade:

[0131] Simulation found that reducing the operating pressure of the flash tank from 3.0 MPa to 2.5 MPa can improve the methanol recovery rate. In actual modification, the pressure control system of the flash tank is adjusted, and a pretreatment step is added to remove CO2.

[0132] By adjusting the key parameters through Aspen Plus simulation, the variable unit model of the coal-to-methanol process can be optimized, providing a scientific basis for modification in practical application. These adjustments not only improve the process efficiency, but also reduce energy consumption and cost, and have important engineering application value.

[0133] In the description of the present application, it should be understood that the terms "center", "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and therefore cannot be understood as indicating or implying that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the present application.

[0134] In addition, the terms "first", "second", etc. are used only to describe different instances, and are not used to indicate or imply relative importance or a number of indications of the technical features indicated. Therefore, the features defined as "first", "second" can explicitly or implicitly include at least one of the features. In the description of the present application, the meaning of "a plurality of" is at least two, such as two, three, etc., unless otherwise explicitly specified.

[0135] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting", "fixing" and the like should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected or in communication with each other; it can be directly connected, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two elements or the interaction relationship between two elements, unless otherwise explicitly limited. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0136] In the present application, unless otherwise explicitly specified and limited, the first feature is "on" or "under" the second feature, which can be direct contact between the first and second features, or indirect contact between the first and second features through an intermediate medium. Moreover, the first feature "above", "above" and "above" the second feature can be directly above or obliquely above the first feature, or only indicate that the horizontal height of the first feature is higher than that of the second feature. The first feature "below", "below" and "below" the second feature can be directly below or obliquely below the first feature, or only indicate that the horizontal height of the first feature is less than that of the second feature.

[0137] In the present application, the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In the present specification, the illustrative description of the above terms does not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any appropriate manner in any one or more embodiments or examples. Furthermore, those skilled in the art can combine and combine different embodiments or examples described in the present specification and the features of different embodiments or examples, without contradiction.

[0138] Although the embodiments of the present application have been shown and described above, it is understood that the above embodiments are exemplary and cannot be construed as limiting the present application, and those skilled in the art can transform, modify, replace and modify the above embodiments within the scope of the present application.

Claims

1. A coal-to-methanol conversion processing system, comprising: The application relates to a coal gasification system. The coal gasification system comprises: a coal gas separator, a flow divider being connected to an outlet of the coal gas separator, water gas in a gasification section entering the coal gas separator, a gas phase discharged from the outlet of the coal gas separator being divided into a first gas phase and a second gas phase by the flow divider; a shift converter, an inlet of the shift converter being connected to the flow divider so that the first gas phase flows into the shift converter, a preheater being arranged between the inlet of the shift converter and the flow divider to heat the first gas phase flowing into the shift converter; a first water separation device, the first water separation device being connected to the flow divider and the shift converter, so that a mixed gas obtained by mixing the second gas phase and a gas stream discharged from the shift converter flows into the first water separation device, the first water separation device being used for multi-stage separation of the mixed gas to obtain shift gas and condensate; a stripping tower, an inlet of the stripping tower being connected to the first water separation device so that at least part of the condensate discharged from the first water separation device flows into the stripping tower, the stripping tower having a steam inlet, steam entering the stripping tower from the steam inlet being in contact with the condensate entering the stripping tower from the first water separation device to recover combustible gas dissolved in the condensate, and condensate discharged from a liquid outlet of the stripping tower flowing back to the gasification section; 2. The coal-to-methanol shift conversion system of claim 1, wherein, a second water separation device, the second water separation device being connected to an outlet of the stripping tower to separate vent gas and waste water.

3. The coal-to-methanol shift conversion system of claim 2, wherein, The coal gasification system further comprises a first mixer, the first mixer being connected to the flow divider and an outlet of the shift converter, a cold side flow channel of the preheater being connected between the flow divider and the inlet of the shift converter, and a hot side flow channel of the preheater being connected between the shift converter and the first mixer.

4. The coal-to-methanol shift conversion system of claim 1, wherein, A first waste heat boiler is arranged between the outlet of the shift converter and the first mixer, and a second waste heat boiler is arranged between an outlet of the first mixer and the first water separation device. The first water separation device comprises: a first water separator, an inlet of the first water separator being connected to the flow divider and the shift converter; a second water separator, an inlet of the second water separator being connected to an outlet of the first water separator, and liquid discharged from liquid outlets of the first water separator and the second water separator flowing back to the gasification section; a third water separator, an inlet of the third water separator being connected to an outlet of the second water separator; 5. The coal-to-methanol shift conversion system of claim 4, wherein, a fourth water separator, an inlet of the fourth water separator being connected to an outlet of the third water separator, and liquid outlets of the third water separator and the fourth water separator being connected to the inlet of the stripping tower. A third waste heat boiler is arranged between the outlet of the first water separator and the inlet of the second water separator, a desalted water heater is arranged between the outlet of the second water separator and the inlet of the third water separator, and a shift gas cooler is arranged between the outlet of the third water separator and the inlet of the fourth water separator; liquid outlets of the first water separator and the second water separator are connected to a second mixer, and an outlet of the second mixer is connected to a first pump.

6. The coal to methanol shift conversion system of claim 4, wherein, The liquid outlet of the third water separator and the liquid outlet of the fourth water separator are connected with a third mixer and a condensate heater, and the condensate heater is connected with the stripping tower so that the condensate discharged from the third mixer flows into the stripping tower after being heated.

7. The coal-to-methanol shift conversion system of claim 6, wherein, The cold side flow channel of the condensate heater is connected between the third mixer and the stripping tower, and the hot side flow channel of the condensate heater is connected to the liquid outlet of the stripping tower so that the liquid flowing out of the liquid outlet of the stripping tower heats the condensate flowing from the third mixer to the stripping tower, and the liquid outlet of the stripping tower is connected with a second pump. And / or, the second water separation device comprises a fifth water separator, the inlet of the fifth water separator is connected with the gas outlet of the stripping tower, and a water cooler is arranged between the inlet of the fifth water separator and the gas outlet of the stripping tower. And / or, the steam inlet comprises a first steam inlet and a second steam inlet, the first steam inlet is used for conveying low-pressure steam in a pipe network into the stripping tower, and the second steam inlet is used for conveying high-pressure flash steam in a gasification section into the stripping tower, and the steam conveyed into the stripping tower flows in a reverse direction with the condensate.

8. A coal-to-methanol shift conversion process simulation method, characterized in that, The coal-to-methanol shift processing system is optimized, and the coal-to-methanol shift processing simulation method comprises: Based on the coal-to-methanol shift processing system, a mathematical model is constructed by using Aspen Plus software; Given the operation information, the mathematical model is run, and a simulation result report is obtained; The actual operation condition is compared with the simulation result report, and the last step is repeated to obtain the final operation information of the mathematical model; At least part of the operation parameters of the mathematical model are adjusted to obtain a target result report; It is judged whether the target result operation meets the requirements; If yes, the actual operation condition parameters of the coal-to-methanol shift processing system are adjusted based on the target result report.

9. The coal-to-methanol shift conversion process simulation method of claim 8, wherein, The step of constructing a mathematical model by using Aspen Plus software comprises: Based on the material composition of water gas, when the temperature is less than or equal to 100 degrees Celsius, the electrolyte property method ELECNRTL is used in the mathematical model of the gas-liquid separation equipment, the liquid phase activity coefficient calculation method is Electrolyte NRTL, and the gas phase fugacity coefficient calculation method is Redlich-Kwong, when the temperature is less than or equal to 100 degrees Celsius, the electrolyte property method RK-SOAVE is used in the mathematical model of the gas-liquid separation equipment; Based on the physical properties and process requirements of each device in the coal-to-methanol shift processing system, corresponding unit operation modules are selected in the Aspen Plus software; Based on the characteristics of heat flow, material flow and power flow in the coal-to-methanol shift processing system, corresponding thermodynamic models and property databases are selected in the Aspen Plus software.

10. The coal-to-methanol shift conversion process simulation method of claim 8, wherein, In the final operation information, the unit operation module adopted by the coal water separator, the first water separator, the second water separator, the third water separator, the fourth water separator and the fifth water separator in the coal-to-methanol shift processing system is Flash2, the unit operation module adopted by the shift furnace in the coal-to-methanol shift processing system is RSoic, the unit operation module adopted by the stripping tower in the coal-to-methanol shift processing system is Flash2, the unit operation module adopted by the first mixer, the second mixer and the third mixer in the coal-to-methanol shift processing system is Mixer, and the unit operation module adopted by the first pump and the second pump in the coal-to-methanol shift processing system is Pump; In the mathematical model built by the AspenPlus software, the operating pressure of the coal water separator is 6.34 MPa, and the operating temperature is 243 degrees Celsius; the operating pressure of the first water separator is 6.06 MPa, and the operating temperature is 216.5 degrees Celsius; the operating pressure of the second water separator is 6.02 MPa, and the operating temperature is 190 degrees Celsius; the operating pressure of the third water separator is 5.97 MPa, and the operating temperature is 106 degrees Celsius; the operating pressure of the fourth water separator is 5.91 MPa, and the operating temperature is 40 degrees Celsius; and the operating pressure of the fifth water separator is 0.41 MPa, and the operating temperature is 45 degrees Celsius; The operating pressure of the shift furnace is 6.14 MPa, and the operating temperature is 441 degrees Celsius; and the operating pressure of the stripping tower is 0.49 MPa, and the operating temperature is 147 degrees Celsius; The outlet pressure of the first mixer is 6.11 MPa, the outlet pressure of the second mixer is 6.02 MPa, the outlet pressure of the third mixer is 0.53 MPa, the outlet pressure of the first pump is 7.2 MPa, and the outlet pressure of the second pump is 1.6 MPa; The unit operation module adopted by the first waste heat boiler, the second waste heat boiler, the third waste heat boiler, the desalted water heater, the shift gas cooler and the water cooler in the coal-to-methanol shift processing system is Heater, a first heat exchange operation module is arranged between the splitter and the inlet of the shift furnace, a second heat exchange operation module is arranged between the outlet of the shift furnace and the first mixer, the first heat exchange operation module and the second heat exchange operation module are connected to constitute a preheater in the coal-to-methanol distillation system, a third heat exchange operation module is arranged between the third mixer and the inlet of the stripping tower, a fourth heat exchange operation module is connected to the liquid outlet of the stripping tower, and the third heat exchange operation module and the fourth heat exchange operation module are connected to constitute a condensate heater in the coal-to-methanol distillation system; and the first heat exchange operation module, the second heat exchange operation module, the third heat exchange operation module and the fourth heat exchange operation module all adopt Heater. In the mathematical model built by the Aspen Plus software, the operating pressure of the first waste heat boiler is 6.11 MPa and the operating temperature is 240 degrees Celsius, the operating pressure of the second waste heat boiler is 6.07 MPa and the operating temperature is 216.5 degrees Celsius, the operating pressure of the third waste heat boiler is 6.03 MPa and the operating temperature is 190 degrees Celsius, the operating pressure of the desalted water heater is 5.98 MPa and the operating temperature is 106 degrees Celsius, the operating pressure of the shift gas cooler is 5.92 MPa and the operating temperature is 40 degrees Celsius, the operating pressure of the water cooler is 0.42 MPa and the operating temperature is 45 degrees Celsius, the operating pressure of the first heat exchange operation module is 6.22 MPa and the operating temperature is 250 degrees Celsius, the operating pressure of the second heat exchange operation module is 6.13 MPa, the operating pressure of the third heat exchange operation module is 0.53 MPa, and the operating pressure of the fourth heat exchange operation module is 0.48 MPa and the operating temperature is 95 degrees Celsius.

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